CN101143274B - Process and device for simulated moving bed seperation with a reduced number of valves - Google Patents
Process and device for simulated moving bed seperation with a reduced number of valves Download PDFInfo
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- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1814—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns recycling of the fraction to be distributed
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- B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
- B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
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Abstract
The invention concerns a simulated moving bed (SMB) separation device comprising a column, beds Ai of adsorbent separated by plates Pi with a single distribution and extraction network for fluids, in particular feed F, desorbant D, raffinate R and extract E, and a plurality of two-way valves for distribution of said fluids, said valves being limited in number compared with the prior art. According to the invention, the column is divided into a plurality of sectors Sk with 2 or 3 superimposed plates, each sector Sk comprising an external bypass line Lk connected to each plate Pi of Sk via a connector comprising a plate valve Vi. Each line Lk comprises a controlled means for limiting its internal flow, and is connected to each of the fluid networks F, D, R, E via a single line comprising a single controlled two-way isolation valve to supply for sequential supply or withdrawal of the corresponding fluid F, D, R or E towards or from the sector Sk under consideration. The invention also concerns a separation process using said device or the use of said device for the separation of para-xylene or meta-xylene from an aromatic C8 cut.
Description
Technical field
The present invention relates to adopt the technical field of distilling the natural or chemical products separation that is difficult to separate.Use class methods and relevant device thereof at present, the method and apparatus that they separate with " chromatogram " or " simulation moving-bed mode " or " simulation reflux type " or " simulation and stream mode " is known, below they is called " SMB ".
The field that relates to not exclusively is:
● normal alkane separates with branched paraffin, cycloalkanes and aromatic compounds;
● the separation of olefin/paraffin;
● other isomers separates in right-xylenes and the C8 aromatic compounds;
●-xylenes and C8 aromatic compounds in the separating of other isomers;
● other isomers separates in ethylbenzene and the C8 aromatic compounds.
Except that refinery and petrochemical complex, have other many application, wherein can enumerate the separation of glucose separation, Cresol Isomers Using, optical isomer etc.
Background technology
The SMB chromatographic isolation is that people know in this technical field.Generally speaking, simulation moving-bedly comprise at least three chromatogram sections, four or five chromatogram sections advantageously, wherein each chromatogram section be constitute by at least one or a part of post and between two supplies or off-take point in succession.Typically, supply with at least a material to be separated material F and strippant D (being sometimes referred to as eluant, eluent), take out at least a raffinate (raffinat) R and extract E.These supplies and off-take point are passed in time and are changed, and typically move to the bed bottom with the method for synchronization.
Many favourable variations can utilize asynchronous exchange to improve the function of this type unit.Simply; Pointed like US-A-5 578 215, the effect that compensates one or more dead volumes for one or more circulating pump is played in these asynchronous exchanges, and is pointed like US-A-5 762 806; Make circulating pump with constant cycle rate work; Eliminating jiggly flow and pressure, or at least two chromatogram sections of last operation, wherein each chromatogram Duan Douyu non-integer absorbent bed equivalence.Pointed like US-A-6 136 198, US-A-6 375 839, US-A-6 712 973 and US-A-6 413 419, this a kind of variation in back is referred to as Varicol.Naturally, can these three kinds of variations be combined.
Be noted that the multichannel rotary valve that entering and effluent fluid are communicated with the bed that places adsorption tower just allows the exchange of wheel synchronization type.For asynchronous exchange, many switch valves are vital.This technical elements is described below.
Prior art has described various device and the method that can in simulation moving-bed, carry out feed separation in detail.Can enumerate US-A-2 985 589, US-A-3 214 247, US-A-3 268 605, US-A-3 592 612, US-A-4 614 204, US-A-4378 292, US-A-5 200 075 and US-A-5 316 821 especially.These patents are also described the function of SMB in detail.
SMB equipment typically comprises at least one tower (often two towers); The chamber Ci that plate Pi will place adsorbent bed Ai and one or more distribution of this tower and/or extract the hydraulic pressure body that gets into each adsorbent bed or come out from each adsorbent bed divides and opens and the control device of continuous dispensing and extraction fluid.
Each plate generally includes a plurality of distributor-blenders-extractor, i.e. and " DME ", they are supplied with through pipeline or " distribution/extraction manifold ".These plates can be any kinds, any geometry, particularly have the panel that in this tower, forms adjacent area; The panel that the angle part is for example arranged, the panel illustrated in fig. 8 of patent US-A-6 537 451 for example, they are that symmetry (manifold) is supplied with; Or parallel zone; The part of for example on circumference, cutting off, like what point out among the publication application US-A-03/0 127 394, they are that disymmetry is supplied with.Preferably, this knockout tower comprises the DME plate of parallel zone and disymmetry supply class.Also preferably, this adsorbent filling is closely knit.Can in certain tower, use more substantial adsorbent like this, improve the purity and/or the SMB flow of required product.
Need the collect stream (along the major cycle fluid of this tower main shaft) of bed of the distribution of each from the front; Might be toward wherein injecting auxiliary fluid or a secondary fluid; Simultaneously these two kinds of fluids are mixed as far as possible; Maybe might remove the fluid that a part is collected, extract it being delivered to this equipment outside, and fluid is redistributed to next bed.
For this reason, in plate Pi, can use distributor chamber Ci, k (injection/extraction), they can separate with mixing chamber or be shared with mixing chamber.Known its has the plate Pi of one or more chambers, perhaps separately supplies with (or taking-up) different fluids in preset time, perhaps supplies with (or taking-up) same fluid simultaneously with abreast in preset time.Under first kind of situation, this plate has a plurality of distribution networks, and it has single distribution network under second kind of situation.The present invention only relates to comprise the equipment of the plate with single distribution network.
Generally speaking, the flow process of perhaps describing according to US-A-2 985 589 lets all fluids or main stream through this tower, and the method for perhaps describing according to US-A-5 200 075 is with major part or outside all this stream is delivered to.
The general considerations of whole SMB equipment is in operation SMB process, when changing supply with off-take point, fluid and plate is supplied with reduced to minimum with the pollution of zones of different of taking out the loop and the generation of the liquid in the volume.In fact, in this operating sequence process, pipeline, chamber or plate Pi supply area are no longer by this method fluid flushing, and it becomes the dead zone of fluid stagnation, and just move when having only other method fluid to move therein again.Because in SMB, this is the diverse ways fluid, must be through having the liquid in the basic different liquid replacement dead zone of forming.Therefore bring and the departing from of ideal operation in the basic different mixing of forming fluids of short time period or circulation, and ideal operation is the discontinuity of forbidding forming.
Therefore another problem possibly be any circulation between the zones of different of same plate, and this also can cause and the departing from of ideal operation.
In order to solve these problems relevant, known different techniques by prior art with recirculation and dead zone:
A) strippant or pure relatively product clean-up line and dead zone have been proposed to use.This technology can avoid polluting this product effectively when extracting its expected product.But the composition of this flushing liquid is very different with the liquid of its replacement usually, and this can bring the discontinuity of composition, and this discontinuity is disadvantageous for ideal operation.This first flushing embodiment is typically carried out " in the flushing of high short time ".Form discontinuous influence in order to limit, these flushings are short time.
B) described like US-A-5 972 224, another solution is to let major part mainly flow in the tower, and few outer bypass line that passes through between adjacent panel that partly should flow flows to the outside, the 2%-20% that normally should flow.Usually in the most of the time or carry out this flushing continuously, so these pipelines and zone no longer be " dead ", but be rinsed.A kind of like this system through bypass line flushing is shown in Fig. 1 of US-A-5 972 224, and in Fig. 1 of the application, simplifies and duplicate.Because these bypass lines are designed to low discharge, therefore they can be minor diameter, and comprise small diameter valve, reduced the cost of system like this.
First advantage of such system is that the injection of a secondary fluid and taking-up loop because this bypass is from adjacent plate on the one hand, are basically continuous rather than discontinuous and wash on the other hand with forming the liquid wash that is in close proximity to replacement liquid.In addition, preferably confirm the flow in these bypass so that the conversion rate in each bypass the pace with concentration gradient during SMB mainly flows is identical basically.Therefore, use on the one hand different pipeline of a kind of fluid flushing and volume, the composition of this fluid basically with pipeline and volume in the composition of liquid identical, and, introduce the liquid that in bypass, circulates again at the essentially identical point of main stream composition.Therefore this second embodiment realizes the long-time flushing of zero-dose gradient " low or ".
Second advantage of this long-time rinse-system (except injection or fetch cycle) is that it can eliminate the influence that possibly recycle between the zone of same plate because of little pressure drop difference.
Relate to the operation of SMB, it typically is a kind of technology of following two big type of technology that the controlled fluid of SMB distributes with extraction equipment:
● perhaps, for each plate, the on-off controlled valve of a plurality of supplies or taking-up fluid; These valves are usually located at the position of the corresponding plate of next-door neighbour; And for each plate Pi, particularly including at least 4 controlled two-way on-off valves, they are corresponding to supplying with fluid F and D and taking out fluid E and R;
● perhaps on all plates, supply with or take out the multichannel rotary valve of fluid.
First kind of technology adopts two-way valve, might produce in batches like this, reaches to improve reliability and low relatively unit cost.Second kind of technology just adopts single valve, but this single valve is a banked direction control valves, but inevitable structure is special, and size is very big, and be also extremely complicated.In addition, this second kind technology got rid of the possibility of asynchronous exchange, as in the Varicol equipment.
The present invention relates to adopt the SMB of conventional two-way valve, promptly adopt the SMB of first kind of technology in two kinds of technology that the front describes.Especially, the present invention relates to improved simulation moving-bed separation equipment, it comprises a plurality of two-way on-off valves, but compared with prior art the quantity of valve has reduced.The present invention can be used for the SMB of synchronous exchange and the SMB of asynchronous exchange, for example Varicol.
Summary of the invention
The present invention relates to improved simulation moving-bed separation equipment, it belongs to the main simulated moving bed technology that uses a plurality of controlled two-way on-off valves (normally with the high standard (sealing/reliability) that requires with the mass-producted standard valve of low cost).
One of them basic purpose of the present invention is to reduce the defective relevant with this type SMB, and this defective is to need a large amount of controlled two-way valves.The present invention can reduce the quantity of these valves, can also keep simultaneously realizing the advantage to effective flushing in dead zone of " long-time under low or zero-dose gradient " type.
Another object of the present invention provides a kind of equipment, and it need reduce the two-way valve of quantity, and does not compared with prior art increase the switching frequency of these valves; This with the valve restricted number that reduces the statistics failure risk, therefore improved the reliability of this system.
At last, in the preferred embodiment of this equipment, can also reduce allowing the quantity of this SMB main fluid with the large-diameter valve of its rated flow circulation.
Equipment of the present invention can be used for new equipment, but also compatible with various existing apparatus, can carry out limited improvement and this equipment is installed on existing apparatus.It is also with various types of compatible with plate Pi geometry, and the plate that for example has the angle part panel or have parallel portion is as long as these plates (or wherein most of plate) are single distribution network types.
Therefore, found a kind of equipment, it can significantly reduce the quantity of main control valve, and these valves are corresponding to the outlet/inlet of this SMB method fluid: in the prior art, each plate all has the major network valve of at least one group of 4 supply/taking-up F, D, R, E.If the fluid more than 4 kinds is arranged, if if two kinds of raffinate R1, R2 are for example arranged or use the phegma RE that is rich in the expectation product, then this quantity also can increase.The bypass line of minor diameter is auxiliary line in the prior art, and fluid F, D, R, E (E1) (E2) (RE) do not supply with or take out these auxiliary lines of flow use with their nominal.
According to the present invention, the major part of this tower or this tower is divided into the section Sk of stack, each section Sk comprises 2 or 3 adsorbent beds and 2 or 3 plates, also comprises bypass line Lk.Opposite with prior art; The fluid of this SMB uses this pipeline Lk with its rated flow; Each tower section (rather than each plate of the prior art) is used unique one group of major network valve (supply with or take out), and these valves are connected with bypass line Lk, to allow these fluids through the Lk circulation.According to the present invention, " plate valve " equipment with restriction bypass flow flow also is provided, but the total quantity of valve still obviously reduces that kind as will be explained below.
The invention still further relates to the SMB separation method that uses the said equipment, be used in particular for from the charging of the aromatic hydrocarbon that contains 8 carbon atoms, separating right-xylenes or-xylenes.
The invention still further relates to the purposes of the said equipment separation of aromatic compounds from the aromatic fraction that contains same carbon number.
The specific embodiment
By understanding the present invention better below in conjunction with the explanation of Fig. 1 (prior art), Fig. 2 and Fig. 3 (equipment of the present invention).
In order to realize one of them above-mentioned purpose, so the present invention proposes a kind of equipment, and it can comprise through simulation moving-bed absorption separating at least one expectation compound from the mixture that contains this compound:
At least one tower; This tower is divided into distributor/extractor plate Pi and divides a plurality of adsorbent bed Ai that open; Supply with fluid to supply with and to extract at least two kinds continuously: charging F and strippant D; At least two kinds are taken out fluids: raffinate R and extract E, Pi place an Ai and next Ai+1 of being right after between
This equipment also comprises at least one charging net F-net, strippant net D-net, raffinate net R-net and extract net E-net; Wherein each Netcom crosses a plurality of intermediate line and is connected with this tower; This intermediate line comprises controlled two-way isolating valve; Be referred to as to net valve, one after the other to supply with or to take out fluid F, D, R, E;
Wherein this tower at least its height major part be divided into a plurality of adjacent stack sections (
superpos é s) Sk; Each section Sk basically by one group at least 2 at the most 5 in succession adsorbent bed and constitute by distributor/extractor plate Pi, these plates Pi is right after and below these adsorbent beds in succession, arranges;
Each distributor/extractor plate Pi of each section (secteur) Sk uses the single public network of supplying with and taking out fluid F, D, R, E continuously;
The plate Pi of each section (
) Sk links together through outer bypass line Lk; And outer bypass line Lk is connected with each plate Pi of Sk through tube connector (embout); This tube connector comprises the single controlled two-way isolating valve that belongs to plate Pi; Be referred to as plate valve Vi, in the past Pi or supply with continuously or take out fluid F, D, R, E by Pi;
Each described bypass line Lk comprises that at least one is limited in the control appliance of circular flow among the Lk (for example control valve+flowmeter+valve program control system), and it perhaps is installed on the pipeline Lk, perhaps in the bypass around the plate Pi of plate valve Vi or Sk;
Wherein the bypass line of each section Sk (ligne de d é rivation) Lk is connected with the E-net with each net F-net, D-net, R-net through single pipeline, and said single pipeline comprises single net valve, is respectively V
Fk, V
Dk, V
Rk, V
Ek, to supply with continuously or to take out corresponding fluids F, D, R, E to the section Sk that is considered or by the section Sk of this consideration;
And the tube connector that comprise plate valve Vi, at least a portion Lk of each plate Pi of its stage casing Sk through connecting, comprise said single net valve, be respectively V
Fk, V
Dk, V
Rk, V
EkSaid single pipeline be connected with sole mode and each net F-net, D-net, R-net and E-net.
Preferably, each section Sk is made up of one group 2 or 3 continuous adsorption agent beds basically.4 or 5 continuous adsorption agent beds cause these towers to have total higher number, can produce different chromatographic zone.
Opposite with the equipment of prior art; Equipment of the present invention can use bypass line Lk; Through unique one group of respective wire valve, rather than have a networking valve like each plate Pi of prior art, will supply with SMB at section Sk with the fluid F of taking out, D, R, E circulation from SMB.Can reduce the control valve total quantity significantly like this, even consider add additional valve, promptly also like this during plate valve Vi.
Above-mentioned control valve: the high-quality metered valve (reliability, sealing, service life) that net valve and plate valve Vi normally carry out the continued operation of SMB.
More generally; Guarantee SMB all control valves of operation (net valve, plate valve Vi continuously; Be limited in the valve of the control device of circular flow among the Lk in addition); " master " valve of the SMB that all should think according to the present invention to be connected with this tower, they through control SMB continuously the system of operation control (computer, programmable device or other equivalent system).
The present invention was unique when the front had been mentioned some main valve of SMB continued operation: the unique networking valve V of the Vi of each plate Pi, every section Sk
Fk, V
Dk, V
Rk, V
EkBut; If also use other valve; For example can control or interim second isolating valve of uncontrollable common poor quality; But they do not participate in the SMB continued operation, and the purpose that they exist is in order to dismantle some equipment (pump that continued operation is used or main valve etc.), all not exceed scope of the present invention.
Usually; Be used for carrying the bypass line Lk of all fluid F, D, R, E with its rated flow; No longer picture little auxiliary line of the prior art in present device; But the maximum gauge of the net valve opening that general internal diameter equals to be connected with Lk at least, the handling capacity not so that let these fluid F, D, R, E circulate.
Since use and can carry the bypass line Lk of high flow capacity, thus the control appliance of limited flow advantageously used, so that reach low discharge bypass circulation (the normally 2%-20% of the motion flow in this tower).Term " bypass circulation " representes that here slave plate takes out the circular flow of one (little) part in this tower, and is incorporated in another plate of same section Sk again.The information that term " control appliance " is applied to provided by flowmeter usually starts the control valve that has the control system usually.For this reason, can use the flow control valve that is directly installed on the pipeline Lk.This valve is open valve gradually normally at this moment, rather than on-off control valve (it has only 2 possible positions: complete opening with close).
But; According to the preferred embodiments of the invention, at least one or preferably each said bypass line Lk comprise the control device that is limited in circular flow among the Lk, it is not to be directly installed on the Lk; But as the bypass around the plate valve Vi of the plate Pi of Sk, at the little second bypass I
KOn.This device generally is control valve vi, and its opening diameter is littler than Vi, and for example diameter equals 60% or 50% of Vi diameter at the most, for example is the 10%-50% of Vi diameter.When getting into flushing and this internal bypass flow as the bypass around the Lk (being recycled to other plate of Sk by the plate of Sk) arranged in limited time, Vi closes with plate valve, opens the little valve vi of bypass around Vi.Therefore, use a plate valve Vi (the valve Vi of the lower plate Pi of Sk usually) the little second bypass I on every side therein
kCan make the valve that can use littler opening diameter, if flow restriction device is the valve that places on the main bypass line Lk, then its diameter is big relatively, because Lk must be able to let fluid F, D, R, E circulate with its rated flow.
According to the present invention, comprise that the tube connector of Vi should be considered to be not included in the Vi little second bypass I on every side
k, do not comprise placing I yet
kOn little valve vi.Therefore this tube connector comprises the single valve Vi that can let main fluid F, D, R, E circulate.
According to first embodiment, at least one section Sk (and all sections Sk) usually is made up of two adsorbent bed Aj, Aj+1 and two distributor/extractor plate Pj, Pj+1, and they are right after respectively and are arranged in below these adsorbent beds.Therefore these sections are 2 beds and 2 plate Pi.
According to second embodiment, at least one section Sk is made up of three adsorbent bed Aj, Aj+1, Aj+2 and three distributor/extractor plate Pj, Pj+1, Pj+2, and they are right after respectively and are arranged in below these adsorbent beds.Therefore these sections are 3 beds and 3 plate Pi.
Should spell out the section Sk definition under situation at the bottom of the tower.In fact, below the adsorbent bed An of tower bottom, there is not plate Pn usually, because need these fluids be assigned in the adjacent next bed.In addition, according to the present invention, suppose that in this case the plate Pn that lacks is replaced by outlet line under this tower, this time outlet line perhaps links to each other with the import of same tower through circulating pump usually, and perhaps the cat head with second knockout tower links to each other.
Preferably, whole tower (except that the cat head plate of being got rid of by the definition of term " section ") is made up of adjacent segment Sk stack.
Therefore all these sections Sk possibly be made up of two adsorbent beds and two distributor/extractor plates, and they are adjacent respectively to be placed on below these adsorbent beds (or think described outlet line is similar with lower plate down).Therefore this tower is made up of the section with 2 beds and 2 plates basically.This tower also possibly be made up of the section with 3 beds and 3 plates basically, or is combined to constitute with the section with 3 beds and 3 plates by the section with 2 beds and 2 plates.At last,, also can comprise of the present invention section Sk and one or more single plate Pi that supplies with according to prior art according to not preferred specific embodiments, represented like Fig. 1.
When not being 4 but 5 or 6 fluid network, for example using 2 kinds of raffinate R1, R2 and/or be rich in the product phegma RE of expectation product, the present invention that also can adopt the front under the situation of 4 fluid F, D, R, E net, to describe in a similar manner.Therefore, each section Sk and pipeline Lk have 5 or 6 net valves.
The invention still further relates to the separation method that uses the said equipment, wherein in cyclic process, sequentially use each pipeline Lk, through plate valve Vi and one of them net valve V of series connection
Fk, V
Dk, V
Rk, V
Ek, with its rated flow fluid F, D, R, E are recycled to each plate Pi of Sk, or eject by each plate Pi of Sk, and wherein in a cyclic process every kind of fluid F, D, R, E use Lk along its whole length.
Generally speaking, during the net opening of valves that is not connected with Lk, at least a portion of each bypass line Lk is carried out interior flushing, during the net opening of valves that is connected with Lk, stops the interior flushing of all Lk.
Preferably; Sk not with whole time cycle that one of them fluid network is connected in and at one of them the net opening of valves that is connected with Sk, a kind of fluid is wherein supplied with plate Pi or is carried out the flushing of Lk from the plate Pi that is arranged in the last position of Sk to being arranged in the plate Pi+1 or the Pi+2 of Sk than upper/lower positions before by wherein a kind of fluid of plate Pi taking-up.Flushing causes in supply or the taking-up (also need open Vi) of plate Pi and opens Vi between the cycle in this, avoids the unlatching of Vi between these consecutive periods or closes.The mobile number that reduces valve has reduced the wearing and tearing of these valves, has improved the reliability of this equipment and correlation technique.
Generally speaking, at least two, often all bypass line Lk carry out interior flushing.Usually, interior flushing accounts at least 20% of the time, and usually at least 40% or even at least 50%.
The present invention can carry out any type chromatographic isolation, particularly separates the method as the right-xylenes of product by the aromatic hydrocarbon charging that contains 8 carbon atoms, or by the aromatic hydrocarbon charging that contains 8 carbon atoms separate as between product-method of xylenes.
Generally speaking, the present invention can make the equipment of front description can be used for from the aromatic hydrocarbon charging that contains identical carbon atoms, separating any aromatic hydrocarbon.
The specific embodiment
Better embodiment of the present invention is such SMB, and its one or more towers are made up of the section Sk with 3 beds and 3 plates basically.In a kind of like this equipment; As the instance of 24 beds and 24 plates (2 towers that for example in the loop, have 12 beds and 12 plates separately), just need 24 plate valves and 4 * 8=32 net valve (8 section Sk, every section needs 4); I.e. 56 main valves; Should add 8 minor adjustment valves (second bypass) toward this main valve, promptly amount to 64 valves, 2.67 valves of each plate average out to.
In the prior art corresponding to Fig. 1, equivalent SMB needs 4 * 24=96 main valve (4 valves of each plate) and 12 swedged valves, promptly amounts to 108 valves, i.e. 4.5 valves of each plate.
The present device of so describing can be used for any chromatography separating method, is used in particular for by the aromatic compounds that contains 8 carbon atoms basically, also contains the charging isolation of aromatic hydrocarbon of this hydrocarbon.
Especially, for example as described in the FR-A-2 789 914, use toluene or right-diethylbenzene as strippant, zeolite is as adsorbent, and this equipment can be used for the right-xylenes of aromatic fraction separation is made up of the C8 hydrocarbon from basically.For example described with patent application FR-A-05/52 485 and FR-A-05/52 486 as US-A-5 900 523, when using toluene or tetrahydronaphthalene as strippant and adsorbent, between this equipment can also be used for isolating from the C8 aromatic fraction-xylenes.
For example use normal butane or pentane as strippant (randomly isooctane is as inert diluent) and 5A zeolite as adsorbent; This equipment can also be used for by hydrocarbon mixture; Particularly alkane or alkane and cycloalkane mixture are isolated one or more normal alkanes (from residual hydrocarbon, separating).
At last, according to condition known to those skilled in the art, for example use the X zeolite that exchanges with calcium, this equipment can also be used for by the hydrocarbon-fraction separating out at least one alkene that contains a kind of like this hydrocarbon.
The invention is not restricted to foregoing description, the technical staff in present technique field can arbitrarily be employed in any other technical characterictic known in this technical field when it is implemented.
Description of drawings
To be more readily understood the present invention by following accompanying drawing with describing, wherein:
Fig. 1 is the sketch map of expression according to the part of prior art SMB equipment, and corresponding net valve is arranged;
The part of Fig. 2 graphic representation SMB equipment of the present invention, it includes the section Sk of 2 beds and 2 plates, and the valve of corresponding net valve, plate valve and restriction bypass flow is arranged;
The part of Fig. 3 graphic representation SMB equipment of the present invention, it includes the section Sk of 3 beds and 3 plates, and the valve of corresponding net valve, plate valve and restriction bypass flow is arranged;
Fig. 4 a, 4b respectively graphic representation have 2 beds and 2 plates the section Sk situation under, the interlude of the tower of present device and end section;
Fig. 4 c, 4d respectively graphic representation have 3 beds and 3 plates the section Sk situation under, the interlude of the tower of present device and end section;
Fig. 5 a and 5b graphic representation respectively are to be placed under the situation of the control valve on the Lk in the flow restriction device of Lk, and the section Sk and the section Sk that 3 beds and 3 plates are arranged of 2 beds and 2 plates arranged.
Referring now to Fig. 1,, it representes a part of chromatograph tower of prior art SMB.Each adsorbent bed Ai-1, Ai, Ai+1, Ai+2, Ai+3, Ai+4 place plate Pi-1, Pi, Pi+1, Pi+2, Pi+3, above the Pi+4, and each plate couples together through valve (mark) each net with 4 fluid network F, D, R, E through pipeline (being respectively 3,4,5,6,7,8).Therefore each plate has 4 main valves.In addition, these plates couple together through bypass line 1a, 1b, 1c in twos, and they comprise small diameter valve, are respectively 2a, 2b, 2c, so that let limited bypass flow pass through: the circular flow in this tower of 2%-20%.Entirely, so each plate Pi has 4 main valves and average 0.5 small diameter valve (2 plate 1), promptly average 4.5 valves of each plate.
The SMB operation of using a kind of like this tower is that the technical staff in present technique field knows.Typically, have no fluid F, D, R, E to supply with 1 plate in 2 plates that connect through bypass line or when wherein taking out (bypass temporarily is in user mode), the valve 2a of bypass line or 2b or 2c open.On the contrary, supply with 1 plate in 2 plates that connect through bypass line or when wherein taking out (bypass is not temporarily used), the valve 2a of bypass line or 2b or 2c close as a kind of fluid F wherein, D, R, E.
Fig. 2 representes a part of tower of present device, and it comprises 3 section Sk, Sk+1, Sk+2, and each comprises that 2 adsorbent beds and 2 tightly are positioned at the plate below the bed.2 plates of every section couple together through bypass line (being respectively Lk, Lk+1, Lk+2), and this bypass line is suitable for letting fluid F, D, R, E with its rated flow circulation.Each bypass line and one group 4 the net valves of supplying with and take out fluid couple together.Opposite with prior art, 4 valves of this group do not provide to 1 plate but offer 2 plates.
Therefore, for first section Sk, 4 net valve V are arranged
Fk, V
Dk, V
Rk, V
EkOffer Pi-1 and Pi.
Each plate also is connected with corresponding bypass line Lk or Lk+1 or Lk+2 through tube connector (corresponding to the horizontal pipeline part on this figure); Tube connector comprises the single two-way control isolating valve (vannes de sectionnement command é es à 2voies) that belongs to this plate, is referred to as plate valve: Vi-1, Vi, Vi+1, Vi+2, Vi+3, Vi+4.Each of section plate valve (Vi, Vi+2, Vi+4) down also has the second little bypass line L
k, L
K+1, L
K+2, they are equipped with the valve of common minor diameter: vi, vi+2, vi+4.
Entirely, each section for 2 plates has 4 net valves, 2 plate valves and 1 small diameter valve in second bypass, i.e. 7 valves, average 3.5 valves of each plate.
This equipment is operated in the following manner:
For example, when in some cycles, wanting, open corresponding net valve V a kind of fluid supply plate Pi-1 among fluid F, D, R, the E or slave plate Pi-1 taking-up for section Sk
Fk, V
Dk, V
Rk, V
EkAnd plate valve Vi-1.Other net valve of this section Sk and Vi and the little second by-passing valve vi close.
In another cycle, when wanting, open corresponding net valve V a kind of fluid supply plate Pi among fluid F, D, R, the E or slave plate Pi taking-up
Fk, V
Dk, V
Rk, V
EkWith plate valve Vi.Other net valve and the Vi-1 of section Sk close.The little second by-passing valve Vi can still close.
In the 3rd cycle, when not wanting, close net valve V a kind of fluid supply plate Pi-1 among fluid F, D, R, the E and Pi or slave plate Pi-1 and Pi taking-up
Fk, V
Dk, V
Rk, V
EkThrough opening Vi-1, close Vi and open little valve vi in second bypass and let limited bypass flow in pipeline Lk, circulate (being injected into the Pi) from the Pi-1 taking-up.Therefore can pass through L
kGuarantee little bypass flow.Vi typically uses the control valve (opening gradually) that unshowned flowmeter is controlled through regulating flow.
Other section Sk+1, Sk+2 operate in a similar manner.
Fig. 3 representes a part of tower of present device, and it comprises 2 section Sk, Sk+1, and every section comprises that 3 adsorbent beds and 3 tightly are positioned at the plate below it.3 plates of every section (are respectively L through bypass line
k, L
k+ 1) couple together, it can let fluid F, D, R, E with its rated flow circulation.Each bypass line is connected with one group of 4 net valve to supply with and to take out fluid.Opposite with prior art, 4 valves of this group do not provide to 1 but offer 3 plates.
Therefore, for first section Sk, 4 net valve V are arranged
Fk, V
Dk, V
Rk, V
EkOffer Pi-1, Pi and Pi+1 simultaneously.
As the equipment of Fig. 2, each plate is connected with corresponding bypass line through the tube connector that comprises plate valve.Each of each section plate valve (Vi+1, Vi+4) down also has little second bypass line, and it installs the valve of common minor diameter: vi+1, vi+4.
This equipment is operated in the following manner:
For example, in some cycles, when supplying with plate Pi-1 or slave plate Pi-1 taking-up to a kind of fluid among fluid F, D, R, the E, open corresponding net valve V for epimere
Fk, V
Dk, V
Rk, V
EkAnd plate valve Vi-1.At this moment other net valve and Vi, Vi+1 and the little second by-passing valve vi of section Sk close.
In another cycle, when wanting, open corresponding net valve V a kind of fluid supply plate Pi among fluid F, D, R, the E or slave plate Pi taking-up
Fk, V
Dk, V
Rk, V
EkWith plate valve Vi.At this moment other net valve of this section Sk and Vi-1 and Vi+1 close.At this moment the little second by-passing valve vi can keep shut.
In the 3rd cycle, when not wanting, close net valve V a kind of supply plate Pi-1 among fluid F, D, R, the E and Pi or slave plate Pi-1 and Pi taking-up
Fk, V
Dk, V
Rk, V
EkAt this moment let limited bypass flow in pipeline Lk, circulate.At this moment two kinds of selections are arranged:
● when opening Vi-1, close Vi and Vi+1 and opening the little valve vi+1 in second bypass, can take out low discharge, be injected among the Pi+1 from Pi-1;
● open Vi, when closing Vi-1 and Vi+1 and opening the little valve vi+1 in second bypass, also can take out the low discharge of Pi, be re-introduced among the Pi+1.
Often, can alternately change the plate that takes out bypass flow (Pi-1, Pi) so that the many plates of flushing most probable.
Preferably, finish last bypass flushing cycle (before supplying with or taking out fluid F, D, R, E) by taking out through upper plate Pi-1.In this case, valve Vi-1 opened in this cycle, did not need this valve to move at the next one when wherein Pi-1 will begin through the cycle that Vi-1 supplies with or takes out, because this valve is opened.
Other section Sk+1, Sk+2 move in a similar manner.
The action type instance of a section Sk (see figure 3) that 3 adsorbent beds and 3 plates are arranged is following, the valve of opening when wherein mentioning the Sk operation, and the valve of not mentioning cuts out:
Cycle 1: the bypass flushing from Pi-1 to Pi+1.Open valve: Vi-1, vi+1;
Cycle2: strippant is injected into Pi-1.Open valve: Vi-1, V
Dk
Cycle3: strippant is injected into Pi.Open valve: Vi, V
Dk
Cycle4: strippant is injected into Pi+1.Open valve: Vi+1, V
Dk
Cycle5: take out raffinate from Pi-1.Open valve: Vi-1, V
Rk
Cycle6: take out raffinate from Pi.Open valve: Vi, V
Rk
Cycle 7: take out raffinate from Pi+1.Open valve: Vi+1, V
RK
Cycle 8: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1;
Cycle 9: by the bypass flushing of Pi-1 to Pi+1.Open valve: Vi, vi+1;
Cycle 10: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1;
Cycle 11: by the bypass flushing of Pi-1 to Pi+1.Open valve: Vi-1, vi+1;
Cycle 12: Pi-1 is injected in charging.Open valve: Vi-1, V
Fk
Cycle 13: Pi is injected in charging.Open valve: Vi, V
Fk
Cycle 14: Pi+1 is injected in charging.Open valve: Vi+1, V
Fk
Cycle 15: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1;
Cycle 16: by the bypass flushing of Pi-1 to Pi+1.Open valve: Vi-1, vi+1;
Cycle 17: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1;
Cycle 18: by the bypass flushing of Pi-1 to Pi+1.Open valve: Vi-1, vi+1;
Cycle 19: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1;
Cycle 20: by the bypass flushing of Pi-1 to Pi+1.Open valve: Vi-1, vi+1;
Cycle 21: take out extract by Pi-1.Open valve: Vi-1, V
Rk
Cycle 22: take out extract by Pi.Open valve: Vi, V
Rk
Cycle 23: take out extract by Pi+1.Open valve: Vi+1, V
Rk
Cycle 24: by the bypass flushing of Pi to Pi+1.Open valve: Vi, vi+1.
Under the situation of the section that 3 adsorbent beds and 3 plates are arranged, confirm that the principle of preferred sequence is following:
1) at every turn by the taking-up of the net valve in bypass line Lk or injection wherein a kind of main fluid (F, D, R, E), this net valve is held open (during 3 cycles in succession) in succession three times.For the first time, this application valve can be connected with upper plate Pi-1, and following plate valve and little bypass flow control valve are all closed.For the second time, middle plate valve can be connected with intermediate plate Pi, and the valve of bunk bed and little bypass flow control valve are closed.For the third time, following plate valve can be connected with lower plate Pi+1, and application valve and rill body bypass control valve (BCV) are closed.
2) injecting or taking out outside the cycle of main fluid (F, D, R, E), bypass flow circulates in Lk.Following plate valve Vi+1 closes, and the little control valve vi+1 that is located in second bypass around the Vi+1 regulates bypass flow through second bypass, and this flow is alternately from upper plate Pi-1 and intermediate plate Pi.In cycle in the end, bypass flow circulates in Lk in supply or before taking out wherein a kind of main fluid, preferably opens application valve Vi-1 (Pi-1 is connected with plate), and can during the next cycle, still open then.
Fig. 4 a and 4b graphic representation have the section of 2 beds and 2 plates.Fig. 4 b is illustrated in a kind of section like this at the bottom of the tower.According to the present invention, suppose that the pipeline that is called Pi+1 substitutes the plate that is located at below the Ai+1 according to definition, does not exist this plate at the bottom of the tower.
Similarly, Fig. 4 c and 4d graphic representation have the section of 3 beds and 3 plates.Fig. 4 d is illustrated in a kind of section like this at the bottom of the tower.According to the present invention, suppose that the pipeline that is called Pi+2 substitutes the plate that is located at below the Ai+2 according to definition, does not exist said plate at the bottom of the tower.
Fig. 5 a and 5b represent to have the section Sk and the section Sk that 3 beds and 3 plates are arranged of 2 beds and 2 plates respectively; Wherein the bypass flow restraint device does not comprise second bypass with valve vi; But have larger-diameter valve 9 and be in pipeline Sk from (having relevant flow measurement device, not shown) on one's body.
Claims (21)
1. equipment through moving-bed adsorption separating at least one expectation compound from contain the mixture of expecting compound, this equipment comprises:
At least one tower; This tower is divided into distributor/extractor plate Pi and divides a plurality of adsorbent bed Ai that open; Supply with fluid to supply with and to extract at least two kinds continuously: charging F and strippant D; At least two kinds are taken out fluids: raffinate R and extract E, Pi place an Ai and next Ai+1 of being right after between
This equipment also comprises fluid network; Be at least a charging net F-net, strippant net D-net, raffinate net R-net and extract net E-net; Wherein each said Netcom crosses a plurality of pipelines and is connected with this tower; This pipeline comprises two-way control isolating valve, is referred to as to net valve, to supply with or to take out said fluid in succession;
Wherein this tower along at least its height major part be divided into a plurality of adjacent stack section Sk; Each section Sk by one group at least 2 at the most 5 in succession adsorbent bed and constitute by distributor/extractor plate Pi, these plates Pi is right after at these and arranges below adsorbent bed in succession;
Each distributor of each section Sk/extractor plate Pi is the single public network of supplying with and taking out fluid F, D, R, E continuously;
The plate Pi of each section Sk will be connected to each other together through outer bypass line Lk; And outer bypass line Lk each plate Pi through tube connector and Sk couples together; This tube connector comprises the single two-way control isolating valve that belongs to plate Pi; Be referred to as plate valve Vi, be used for supplying with or take out fluid F, D, R, E continuously toward Pi or by Pi;
Each described bypass line Lk comprises that at least one is limited in the control device of circular flow among the Lk, and it perhaps is installed on the pipeline Lk, perhaps in the bypass around the plate valve Vi of the plate Pi of Sk;
Wherein the bypass line Lk of each section Sk is connected with the E-net with each net F-net, D-net, R-net through single pipeline, and said single pipeline comprises single net valve, is respectively V
Fk, V
Dk, V
Rk, V
Ek, be used for supplying with or take out corresponding fluids F, D, R or E continuously to the section Sk that considers or by the section Sk that considers;
And the tube connector that comprise plate valve Vi of each plate Pi of its stage casing Sk through being connected in series, at least a portion Lk then, comprise said single net valve then, be respectively V
Fk, V
Dk, V
Rk, V
EkSaid single pipeline be connected with sole mode and each net F-net, D-net, R-net and E-net.
2. equipment according to claim 1, wherein each section Sk is made up of one group of 2 or 3 adsorbent bed in succession.
3. equipment according to claim 1 and 2, wherein the maximum open diameter of the internal diameter of the bypass line Lk net valve that equals at least to be connected with Lk.
4. equipment according to claim 1 and 2, wherein at least one section Sk is made up of two adsorbent bed Aj, Aj+1 and two distributor/extractor plate Pj, Pj+1, and said plate is right after respectively and places below these adsorbent beds.
5. equipment according to claim 1, wherein at least one section Sk is made up of three adsorbent bed Aj, Aj+1, Aj+2 and three distributor/extractor plate Pj, Pj+1, Pj+2, and said plate is right after respectively and places below these adsorbent beds.
6. equipment according to claim 1 and 2, wherein whole tower are that the section Sk by described adjacent stack constitutes, this tower comprise with corresponding to the similar following outlet line of plate Pn that descends adsorbent bed An.
7. equipment according to claim 4, wherein all section Sk are made up of with two distributors/extractor plate or described similar following outlet line two adsorbent beds, said plate be right after respectively place these adsorbent beds below.
8. equipment according to claim 2, wherein each said bypass line Lk comprises the control device of circular flow among at least one restriction Lk, the bypass of its conduct around the plate valve Vi of the plate Pi of Sk installed.
9. equipment according to claim 8, wherein the said device as circular flow among the restriction Lk of the installation of the bypass around said plate valve Vi comprises control valve, its opening diameter is less than the opening diameter of Vi.
10. equipment according to claim 5; Wherein for each section Sk with three plate Pj, Pj+1, Pj+2; Bypass line Lk comprises first device of the circular flow that is limited between Pj and the Pj+1, is limited in second device of the circular flow between Pj+1 and the Pj+2.
11. use method, wherein in a cyclic process, through plate valve Vi and one of them net valve V of series connection according to the said device separates product of each claim in the aforesaid right requirement
Fk, V
Dk, V
Rk, V
EkUse each pipeline Lk fluid F, D, R, E to be recycled to each plate Pi of Sk with their rated flow sequentially; Or from each plate Pi circulation of fluid F, D, R, the E of Sk, wherein each fluid F, D, R, E use Lk on the whole length of Lk in a cyclic process.
12. method according to claim 11, during the net opening of valves that wherein is not connected with Lk, at least a portion of each bypass line Lk is carried out interior flushing, when the net opening of valves that is connected with Lk, stops the interior flushing of all Lk.
13. according to claim 11 or 12 described methods; Wherein, Sk not with whole time cycle that one of them fluid network is connected in and one of them the net opening of valves that is connected with Sk with the cycle next-door neighbour that is used for supplying with or take out a kind of fluid wherein to plate Pi or by plate Pi before from be arranged in Sk than on the position plate Pi and carry out the flushing of Lk to being positioned at the plate Pi+1 or the Pi+2 of Sk than upper/lower positions.
14. according to claim 11 or 12 described methods, wherein at least 2 bypass line Lk wash.
15., wherein in this tower, carry out the supply of fluid F, D, R, E and the asynchronous exchange of off-take point according to claim 11 or 12 described methods.
16. method according to claim 15 is wherein used the said equipment that the chromatogram zone is arranged, wherein the adsorbent bed of at least some regional right and wrong integers equivalence.
17. according to claim 11 or 12 described methods, this method is used for by containing 8 carbon atoms and containing the aromatic compounds charging isolation of aromatic hydrocarbon of hydrocarbon.
18. method according to claim 17, this method are used for separating right-xylenes by the aromatic hydrocarbon charging that contains 8 carbon atoms.
19. method according to claim 17, this method are used for by the aromatic hydrocarbon charging compartment-xylenes that contains 8 carbon atoms.
20. use according to the described equipment of each claim among the claim 1-10 method of separating said hydrocarbon by the hydrocarbon charging that contains at least a normal alkane.
21. use according to the described equipment of each claim among the claim 1-10 method of separating said hydrocarbon by the hydrocarbon charging that contains at least a olefin(e).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR06/07272 | 2006-08-08 | ||
| FR0607272A FR2904776B1 (en) | 2006-08-08 | 2006-08-08 | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMUL WITH A REDUCED NUMBER OF VALVES |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101143274A CN101143274A (en) | 2008-03-19 |
| CN101143274B true CN101143274B (en) | 2012-03-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007101399911A Expired - Fee Related CN101143274B (en) | 2006-08-08 | 2007-08-07 | Process and device for simulated moving bed seperation with a reduced number of valves |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US7582206B2 (en) |
| KR (1) | KR101444944B1 (en) |
| CN (1) | CN101143274B (en) |
| BR (1) | BRPI0703338B1 (en) |
| DE (1) | DE102007036830B4 (en) |
| FR (1) | FR2904776B1 (en) |
| NL (1) | NL1034239C2 (en) |
| RU (1) | RU2448755C2 (en) |
Families Citing this family (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2904776B1 (en) * | 2006-08-08 | 2009-01-23 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMUL WITH A REDUCED NUMBER OF VALVES |
| FR2907021B1 (en) * | 2006-10-16 | 2009-02-06 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMULATED AT A NUMBER OF LOW DIAMETER REDUCED VALVES |
| FR2913346B1 (en) * | 2007-03-09 | 2009-04-24 | Inst Francais Du Petrole | MOBILE BED SEPARATION METHOD AND DEVICE SIMULATED WITH NUMBER OF LARGE DIAMETER VALVES AND REDUCED LINE VOLUME |
| FR2913345B1 (en) * | 2007-03-09 | 2010-06-11 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMUL WITH A NUMBER OF VALVES AND A VOLUME OF REDUCED LINES |
| FR2930174B1 (en) * | 2008-04-17 | 2010-04-30 | Inst Francais Du Petrole | IMPROVED SIMUL MOBILE BED SEPARATION DEVICE |
| FR2935101B1 (en) * | 2008-08-19 | 2011-04-08 | Inst Francais Du Petrole | METHOD AND DEVICE FOR MOBILE BED SEPARATION SIMULATED AT AUTOMATICALLY NOT AUTOMATICALLY ADJUSTED FLUID FLOW RATE |
| US20100047145A1 (en) * | 2008-08-21 | 2010-02-25 | Corning Incorporated | Systems And Methods For Removing Contaminants From Fluid Streams |
| FR2944215B1 (en) * | 2009-04-10 | 2011-04-01 | Inst Francais Du Petrole | SIMPLE MOBILE BED SEPARATION METHOD AND DEVICE HAVING TWO BED DERIVATION LINES AND MODULE DERIVATION FLUID FLOW RATE |
| KR101036554B1 (en) * | 2009-11-16 | 2011-05-24 | 인하대학교 산학협력단 | A method for starting up simulated moving bed chromatography in an asynchronous way |
| CN102895799B (en) * | 2011-07-28 | 2015-09-23 | 中国石油化工股份有限公司 | The moving-bed adsorption separation method that control valve quantity reduces and equipment |
| CN103058817B (en) * | 2011-10-19 | 2014-12-31 | 中国石油化工股份有限公司 | Method for establishing aromatic hydrocarbon production flow model |
| KR101321987B1 (en) * | 2012-06-19 | 2013-10-28 | 인하대학교 산학협력단 | The seperation method of mid-affirnity component material to desorbent from ternary system using center-cut simulated moving bed chromatography |
| US9162205B2 (en) | 2012-12-31 | 2015-10-20 | Uop Llc | Apparatuses for distributing fluids in fluidized bed reactors |
| CN104511183B (en) * | 2013-09-29 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of moving-bed adsorption separation method |
| CN104511184B (en) * | 2013-09-29 | 2016-07-06 | 中国石油化工股份有限公司 | A kind of adsorbing separation C8The pipeline flushing method of aromatic hydrocarbons simulation used moving bed |
| WO2016148755A1 (en) | 2015-03-19 | 2016-09-22 | Exxonmobil Chemical Patents Inc. | Process and apparatus for the production of para-xylene |
| CN106237651B (en) * | 2016-08-31 | 2018-04-27 | 山东新和成氨基酸有限公司 | A kind of method and its device of liquid-solid system Dynamic Adsorption |
| RU2637960C1 (en) * | 2017-02-28 | 2017-12-08 | Федеральное государственное бюджетное учреждение науки Институт общей и неорганической химии им. Н.С. Курнакова Российской академии наук (ИОНХ РАН) | Recirculation method of extraction-chromatographic separation of components mixture |
| JP2020509387A (en) * | 2017-03-03 | 2020-03-26 | ブリガム・ヤング・ユニバーシティＢｒｉｇｈａｍ Ｙｏｕｎｇ Ｕｎｉｖｅｒｓｉｔｙ | Multi-mode multi-detector liquid chromatography system |
| FR3082755B1 (en) * | 2018-06-20 | 2022-12-30 | Ifp Energies Now | METHOD AND DEVICE FOR SEPARATION IN A SIMULATED MOBILE BED WITH A REDUCED NUMBER OF BEDS WITH DERIVATIVE FLUID FLOW |
| US11027221B2 (en) | 2018-10-19 | 2021-06-08 | Uop Llc | Process for a dual extract flush |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1072922A (en) * | 1991-09-05 | 1993-06-09 | 法国石油公司 | Adopt the method and apparatus of simulated moving bed adsorption and crystallization separating paraxylene from eight carbon aromatic hydrocarbons |
| CN1107381A (en) * | 1994-12-07 | 1995-08-30 | 中国石化扬子石油化工公司 | Improved adsorption separation process for simulation moving bed |
| CN1126628A (en) * | 1994-06-17 | 1996-07-17 | 代科化学工业株式会社 | Simulated moving bed chromatographic separation process |
| US6156197A (en) * | 1998-09-02 | 2000-12-05 | Institut Francais Du Peetrole | Fluid distributing-collecting system and its process |
| EP1325772A1 (en) * | 2001-12-19 | 2003-07-09 | Institut Francais Du Petrole | System for injecting a by-pass fluid in a separation methof in a simulated moving bed |
| CN1714915A (en) * | 2004-05-25 | 2006-01-04 | 法国石油公司 | Improved simulated moving bed separation process and device |
Family Cites Families (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3214247A (en) * | 1963-02-25 | 1965-10-26 | Universal Oil Prod Co | Fluid distributing means for packed chambers |
| US4434051A (en) * | 1982-06-07 | 1984-02-28 | Uop Inc. | Multiple valve apparatus for simulated moving bed adsorption processes |
| SU1414316A3 (en) * | 1983-09-07 | 1988-07-30 | Юоп Инк,(Фирма) | Method of separating a mixture of oleic and linoleic acids |
| US5200075A (en) * | 1991-03-08 | 1993-04-06 | Nkk Corporation | Separator |
| FR2721528B1 (en) * | 1994-06-22 | 1996-09-06 | Inst Francais Du Petrole | Separation process by simulated moving bed chromatography with dead volume correction by desynchronization of the periods. |
| US5635072A (en) * | 1995-01-31 | 1997-06-03 | Uop | Simulated moving bed adsorptive separation process |
| FR2751888B1 (en) * | 1996-07-31 | 1998-09-11 | Inst Francais Du Petrole | DEVICE AND METHOD FOR RINSING A SIMULATED MOBILE BED COMPRISING AT LEAST TWO FLUID DELIVERY LINES |
| FR2757507B1 (en) * | 1996-12-20 | 1999-01-29 | Inst Francais Du Petrole | PARAXYLENE SEPARATION PROCESS COMPRISING ADSORPTION WITH WATER INJECTION AND CRYSTALLIZATION |
| FR2772634B1 (en) * | 1997-12-22 | 2000-02-18 | Inst Francais Du Petrole | METHOD AND DEVICE FOR IMPROVING THE PURITY OF A SIMULATED MOBILE BED PRODUCT |
| FR2774310B1 (en) * | 1998-02-02 | 2000-02-25 | Inst Francais Du Petrole | DEVICE FOR DISCONTINUOUS INJECTION OF A FLUID F2 INTO ZONE Z1 OR FOR DISCONTINUOUS EXTRACTION OF A FLUID F1 FROM A ZONE Z1 |
| FR2777798B1 (en) * | 1998-04-27 | 2000-06-02 | Inst Francais Du Petrole | METHOD AND DEVICE FOR IMPROVING THE PURITY OF A SIMULATED MOBILE BED PRODUCT INCLUDING FORCED FLUID RECIRCULATION |
| FR2781860B1 (en) * | 1998-07-31 | 2000-09-01 | Inst Francais Du Petrole | ALTERNATE COMMUNICATION SYSTEM OF AT LEAST FOUR FLUIDS AND ITS APPLICATION IN A SIMULATED MOBILE BED SEPARATION PROCESS |
| FR2782656B1 (en) * | 1998-09-02 | 2000-09-29 | Inst Francais Du Petrole | FLUID DISPENSER-MIXER-EXTRACTOR AND RELATED METHOD |
| FR2785196B1 (en) * | 1998-10-29 | 2000-12-15 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATION WITH VARIABLE LENGTH CHROMATOGRAPHIC AREAS |
| US6413419B1 (en) * | 1998-10-29 | 2002-07-02 | Institut Francais Du Petrole | Process and device for separation with variable-length chromatographic |
| FR2794836B1 (en) * | 1999-06-09 | 2001-08-03 | Inst Francais Du Petrole | IMPROVED ROTARY VALVE |
| FR2794663B1 (en) * | 1999-06-09 | 2001-07-13 | Inst Francais Du Petrole | DEVICE FOR INJECTING A DEVIED FLUID INTO A SIMULATED MOBILE BED SEPARATION PROCESS |
| FR2843893B1 (en) * | 2002-08-28 | 2004-10-15 | Inst Francais Du Petrole | METHOD FOR OPTIMIZING THE OPERATION OF A XYLENE SEPARATION UNIT BY SIMULATED COUNTER-CURRENT |
| FR2904776B1 (en) * | 2006-08-08 | 2009-01-23 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMUL WITH A REDUCED NUMBER OF VALVES |
| FR2907021B1 (en) * | 2006-10-16 | 2009-02-06 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMULATED AT A NUMBER OF LOW DIAMETER REDUCED VALVES |
| FR2913345B1 (en) * | 2007-03-09 | 2010-06-11 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SEPARATING A MOBILE BED SIMUL WITH A NUMBER OF VALVES AND A VOLUME OF REDUCED LINES |
-
2006
- 2006-08-08 FR FR0607272A patent/FR2904776B1/en not_active Expired - Fee Related
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2007
- 2007-08-03 DE DE102007036830.7A patent/DE102007036830B4/en not_active Expired - Fee Related
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- 2007-08-07 CN CN2007101399911A patent/CN101143274B/en not_active Expired - Fee Related
- 2007-08-07 US US11/890,526 patent/US7582206B2/en not_active Expired - Fee Related
- 2007-08-08 KR KR1020070079828A patent/KR101444944B1/en active IP Right Grant
- 2007-08-08 NL NL1034239A patent/NL1034239C2/en not_active IP Right Cessation
- 2007-08-08 BR BRPI0703338-9A patent/BRPI0703338B1/en not_active IP Right Cessation
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1072922A (en) * | 1991-09-05 | 1993-06-09 | 法国石油公司 | Adopt the method and apparatus of simulated moving bed adsorption and crystallization separating paraxylene from eight carbon aromatic hydrocarbons |
| CN1126628A (en) * | 1994-06-17 | 1996-07-17 | 代科化学工业株式会社 | Simulated moving bed chromatographic separation process |
| CN1107381A (en) * | 1994-12-07 | 1995-08-30 | 中国石化扬子石油化工公司 | Improved adsorption separation process for simulation moving bed |
| US6156197A (en) * | 1998-09-02 | 2000-12-05 | Institut Francais Du Peetrole | Fluid distributing-collecting system and its process |
| EP1325772A1 (en) * | 2001-12-19 | 2003-07-09 | Institut Francais Du Petrole | System for injecting a by-pass fluid in a separation methof in a simulated moving bed |
| CN1714915A (en) * | 2004-05-25 | 2006-01-04 | 法国石油公司 | Improved simulated moving bed separation process and device |
Also Published As
| Publication number | Publication date |
|---|---|
| NL1034239C2 (en) | 2008-04-22 |
| KR20080013819A (en) | 2008-02-13 |
| NL1034239A1 (en) | 2008-02-11 |
| DE102007036830B4 (en) | 2017-07-06 |
| US20080041788A1 (en) | 2008-02-21 |
| KR101444944B1 (en) | 2014-09-26 |
| CN101143274A (en) | 2008-03-19 |
| RU2007130237A (en) | 2009-02-20 |
| FR2904776A1 (en) | 2008-02-15 |
| BRPI0703338A (en) | 2008-04-01 |
| DE102007036830A1 (en) | 2008-02-14 |
| RU2448755C2 (en) | 2012-04-27 |
| BRPI0703338B1 (en) | 2018-06-05 |
| FR2904776B1 (en) | 2009-01-23 |
| US7582206B2 (en) | 2009-09-01 |
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